WO2014196611A1 - Dispositif de concentration et procédé de concentration - Google Patents

Dispositif de concentration et procédé de concentration Download PDF

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Publication number
WO2014196611A1
WO2014196611A1 PCT/JP2014/065007 JP2014065007W WO2014196611A1 WO 2014196611 A1 WO2014196611 A1 WO 2014196611A1 JP 2014065007 W JP2014065007 W JP 2014065007W WO 2014196611 A1 WO2014196611 A1 WO 2014196611A1
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WIPO (PCT)
Prior art keywords
stock solution
heat
steam
heat exchanger
amount
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PCT/JP2014/065007
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English (en)
Japanese (ja)
Inventor
大川原　正明
源太郎 根本
寂樹 甘蔗
堤　敦司
真典 石束
寛之 水野
Original Assignee
大川原化工機株式会社
国立大学法人東京大学
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Priority to JP2015521494A priority Critical patent/JP6692059B2/ja
Publication of WO2014196611A1 publication Critical patent/WO2014196611A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid

Definitions

  • the present invention relates to a concentration apparatus.
  • the present invention relates to a concentration apparatus that can be used in a concentration process in the field of foods, preparations, and pharmaceuticals.
  • the recompression method has been proposed for a long time, it has not been completed as a system and has not been widely spread. This is because the compressor used in the recompression method is expensive for the entire apparatus. Other reasons include the difficulty in securing an effective heat transfer area by scaling, the problem of tracking of control equipment, the absence of a device that ensures the cleanliness of the heat transfer area, For example, there were insufficient studies.
  • Patent Document 1 a heating module aimed at realizing an energy saving effect.
  • This heating module lowers the temperature of the input fluid by expanding the input fluid with an expander. And when this temperature falls, it is comprised as heating energy which can collect
  • Patent Document 1 discloses a “first heat exchanger” that exchanges heat between an input fluid and an output fluid, and a “first compressor” that compresses one of the input fluid and the output fluid to raise the temperature. ”And an expander that lowers the temperature by expanding the input fluid.“ Heating module ”is described. The “heating module” of Patent Document 1 aims to enhance the energy saving effect.
  • Patent Document 2 a separation process module has been proposed in relation to the prior art, and a high energy saving effect is obtained (Patent Document 2). That is, according to the separation process module of Patent Document 2, in the first heat exchanger, the input fluid flowing through the combined flow path is heated by the first output fluid compressed by the first compressor. Further, in the second heat exchanger, the input fluid flowing through the first branch path is heated by the first output fluid that has passed through the first heat exchanger. In the third heat exchanger, the temperature of the input fluid flowing through the second branch path is increased by the second output fluid. With such a configuration, work of a predetermined energy is required when the first output fluid is compressed by the first compressor, but it is almost unnecessary to separately heat the input fluid flowing through the combined flow path in a heating furnace such as a boiler. , And.
  • Patent Document 2 discloses a “separator” that separates an input fluid including a first component and a second component into a first output fluid including a first component and a second output fluid including a second component. And a “first compressor” that raises the temperature by compressing the first output fluid output from the separator. Further, the “separation process module” includes a first heat exchanger, a second heat exchanger, and a third heat exchanger. The “separation process module” of Patent Document 2 aims to enhance the energy saving effect.
  • Patent Documents 1 and 2 can be evaluated in terms of improving energy efficiency, but are not suitable for concentrating undiluted solutions in the food, pharmaceutical and pharmaceutical fields.
  • Patent Documents 1 and 2 when concentrating a stock solution, due to a problem caused by property change when the stock solution proceeds, a problem in operation such as continuing steady operation is handled. It is difficult to do.
  • Patent Documents 1 and 2 due to scaling that precipitates when the unconcentrated stock solution including food and pharmaceuticals is concentrated, it adheres to the surface of the heat transfer tube, and the efficiency of heat exchange decreases due to a decrease in heat transfer efficiency. It is difficult to solve such problems.
  • the present invention has been made to solve the above problems, and provides a concentrating apparatus and a concentrating method by an evaporation method that can dramatically reduce the energy to be input as compared with a conventional heating method.
  • a three-phase fluidized bed operation with high thermal efficiency is possible, scaling of the heat transfer surface can be prevented, and operation can be performed even when the concentration of the concentrate is high.
  • An apparatus and a concentration method are provided.
  • the present invention provides the following concentration apparatus and concentration method.
  • a steam recompressor capable of generating pressurized steam obtained by pressurizing steam, the amount of liquid sensible heat of the concentrate to be concentrated, and the amount of liquid sensible heat after the pressurized steam is condensed
  • the sensible heat amount of the concentrate after the concentrate is concentrated can be exchanged, from the first heat exchanger, the amount of heat of the pressurized steam, the amount of latent heat of evaporation of the stock solution, and the stock solution
  • a second heat exchanger capable of exchanging the amount of sensible heat of the evaporated vapor and concentrating the stock solution; supplying the stock solution to the first heat exchanger; and Stock solution supply means for supplying the second heat exchanger from the heat exchanger, steam supply means for supplying the vapor evaporated from the stock solution to the second heat exchanger, and discharging the concentrated solution concentrated from the stock solution to the outside
  • the first discharging means, and the second heat exchanger that has flowed out of the stock solution Comprising a water separator means for separating the mixed in the gas water droplets, a
  • the second heat exchanger includes a heat transfer area for concentrating the raw material, and the heat transfer area of the heat transfer area is formed so as to be changeable.
  • Retransmission means for concentrating the stock solution and retransmitting the obtained concentrated stock solution to one of the second heat exchanger and the first heat exchanger [1] to [5] The concentrator according to any one of the above.
  • Pressurized steam generation process for generating pressurized steam by pressurizing steam, the amount of liquid sensible heat of the stock solution to be concentrated, and the amount of heat of liquid sensible heat after the pressurized steam is condensed
  • the first heat exchange step of exchanging the amount of sensible heat of the concentrated solution in which the stock solution is concentrated, the amount of heat of the pressurized steam, the amount of latent heat of vaporization of the stock solution, and the sensible heat of vapor evaporated from the stock solution A second heat exchange step capable of concentrating the stock solution, and supplying the stock solution to the first heat exchange step, and further, from the first heat exchange step, A stock solution supply step for supplying to the second heat exchange step, a steam supply step for supplying the vapor evaporated from the stock solution to the second heat exchange step, and a first discharge step for discharging the concentrated solution concentrated from the stock solution to the outside.
  • the concentration operation can be performed efficiently by exchanging heat between the sensible heat and the latent heat in the concentration operation of the stock solution, and the energy input compared to the conventional heating method Can be provided with a concentrating device and a concentrating method.
  • the present invention is characterized in that, as the concentration operation proceeds, the properties of the concentrated stock solution and the heat exchange conditions change, but the operation can be performed stably and energy saving.
  • by using a three-phase fluidized bed it is possible to operate with high thermal efficiency, improve energy efficiency, and perform a concentration operation using a steam recompression technique using a steam compressor such as a steam compressor or a steam compression blower.
  • a concentrating device and a concentrating method can be provided.
  • the concentration apparatus of the present invention broadly encompasses concentrators having the invention-specific matters, and is not limited to the following embodiments.
  • the concentrator in the present invention generally comprises a steam recompressor, a first heat exchanger, a second heat exchanger, a stock solution supply means, a steam supply means, a first discharge means, a water droplet separation means, and a second discharge means, It is configured as a concentrator for concentrating the stock solution.
  • the “steam recompressor” can generate pressurized steam obtained by pressurizing steam.
  • the “first heat exchanger” includes the amount of liquid sensible heat of the concentrate to be concentrated, the amount of liquid sensible heat after the pressurized steam is condensed, and the amount of sensible heat after the concentrate is concentrated. The amount of heat can be exchanged, and the stock solution to be concentrated is heated.
  • the “second heat exchanger” can exchange the amount of heat of the pressurized steam, the amount of latent heat of evaporation of the stock solution, and the amount of sensible heat of the vapor evaporated from the stock solution, and can concentrate the stock solution.
  • the “stock solution supply means” is means for supplying the stock solution to the first heat exchanger and further supplying the stock solution from the first heat exchanger to the second heat exchanger.
  • the “steam supply means” is means for supplying the vapor evaporated from the stock solution to the second heat exchanger.
  • the “first discharge means” is a means for discharging the concentrated liquid obtained by concentrating the stock solution to the outside.
  • the “water droplet separating means” is means for separating water droplets mixed in the vapor that has flowed out from the second heat exchanger and evaporated from the stock solution.
  • the “second discharge means” is a means for discharging the liquid after the pressurized vapor is condensed.
  • the concentrating device of the present invention can perform the concentrating operation by a self-heat regeneration technique using a steam recompressor such as a compressor or a steam compression blower. Furthermore, in the concentration apparatus of the present invention, a highly efficient concentration operation can be realized by exchanging all of liquid sensible heat, latent heat of vaporization, and steam sensible heat in the concentration / evaporation process. In addition, since only the temperature difference required for heat exchange becomes the energy required as power, the concentration process using the concentration apparatus of the present invention can perform the concentration process without requiring a new heating operation. To do. In the present invention, it is possible to cope with a change in the properties of the stock solution accompanying the progress of the concentration operation, and it is possible to suppress the scaling on the heat exchange surface. High operation is possible.
  • the steam recompressor (compressor) according to the present invention generates pressurized steam by pressurizing steam. That is, the vapor recompressor is used to recompress the vapor supplied in the path of the concentrator.
  • a vapor recompressor include a compressor and a vapor compression blower.
  • steam-compatible compressor steam compressor
  • the concentration operation can be performed by the self-heat regeneration technology using a steam compressor, energy efficiency can be improved.
  • the steam compressed and pressurized by the steam recompressor is preferably steam generated in the process of evaporating the stock solution.
  • steam introduced into the concentrator may be used, but it is preferable to use the steam generated in the process of evaporating the stock solution in the treatment process.
  • the higher the proportion of steam generated in the process of evaporating the stock solution the more energy efficiency can be improved. Therefore, the steam is more likely to be generated in the process of evaporating the stock solution. preferable.
  • steam is supplied to the inside of the apparatus by steam generating means such as a boiler to give residual heat in the path of the concentrator, from the start of the concentrator to the steady operation in which the concentrate is concentrated. It is preferable.
  • the “steam recompressor” is preferably capable of increasing the amount of heat by recompressing the “steam”. Increase energy efficiency by increasing the amount of heat exchange temperature difference to pressurized steam by a steam recompressor, and exchanging the increased amount of heat with the amount of undiluted solution in the concentrator. Because.
  • the above-mentioned “vapor recompressor” generates the total amount of heat necessary for the concentration treatment of the stock solution to be concentrated. By being configured in this way, the energy efficiency can be maximized.
  • the “first heat exchanger” in the present invention is the amount of liquid sensible heat of the stock solution to be concentrated, the amount of sensible heat of the liquid after the pressurized steam is condensed, and the concentration after the stock solution is concentrated.
  • the sensible heat of the liquid is configured to be exchangeable for both heat amounts. In other words, it is provided for exchanging sensible heat in the path from “supply of the stock solution” to the concentrator to the discharge of “concentrate” from the concentrator and “liquid after condensed pressurized vapor”. .
  • the “first heat exchanger” is described as one device, but after the pressurized steam is condensed with respect to the amount of heat of liquid sensible heat of the stock solution to be concentrated.
  • independent heat exchangers may be used.
  • the “second heat exchanger” in the present invention can exchange the amount of heat of pressurized steam, the amount of latent heat of evaporation of the stock solution, and the amount of sensible heat of the vapor evaporated from the stock solution, and can concentrate the stock solution It is.
  • the “second heat exchanger” in this way together with the “first heat exchanger”, liquid sensible heat and latent heat of vaporization are obtained in the evaporation process when the concentrate is obtained by concentrating the stock solution. All of the steam sensible heat can be exchanged. Therefore, a highly efficient heat exchange operation can be realized.
  • “stock solution” is stored in “stock solution tank 17 a” constituting stock solution supply means 17, and a predetermined amount is sent to “first heat exchanger 5” by pump P.
  • a “concentrator 1” configured as described above can be cited.
  • the “stock solution” heated by the “first heat exchanger 5” is further passed through the “stock solution supply pipe 17 c” constituting the stock solution supply means 17 to the “first solution exchanger 17”. It is configured to be fed to the 2 heat exchanger 7 ”.
  • the “second heat exchanger 7” is connected to the first discharge pipe 21d, which is the “first discharge means 21” for discharging the concentrate to the outside via the first heat exchanger 5. ing.
  • the concentrated stock solution is recovered in the concentrate recovery tank 21a.
  • the concentration and purity of the recovered stock solution may be low.
  • it is recovered in the auxiliary tank 21b.
  • the “second heat exchanger 7” is connected to a second discharge pipe or the like, which is a “second discharge means 23 for discharging the liquid after the pressurized steam is condensed. From the “second heat exchanger 7”, steam containing water droplets / splashes is introduced into the separator 25, and water droplets / splashes contained in the steam are separated.
  • 1 is shown, 1 step
  • the water droplets / splashes separated here are collected in the concentrated liquid collection tank 21a via the first discharge pipe 21d.
  • the steam from which water droplets / splashes are separated is introduced into the compressor 3 and the blower 13 via the first circulation line 9.
  • the inside of the device is in the state of outside air, so the initial replacement steam is introduced from the front of the separator, and the interior of the device is replaced with steam before shifting to steady operation. .
  • the shape of the “second heat exchanger” in the present invention can be, for example, a plate heat exchanger.
  • the plate heat exchanger can easily change the heat transfer area by changing the number of plates, and is suitable when the heat transfer area needs to be changed depending on operating conditions.
  • the “second heat exchanger” is preferably a three-phase fluidized bed.
  • the three-phase fluidized bed is a fluidized bed in which a solid phase (fluid medium or precipitate such as glass beads), a gas phase (vapor), and a liquid phase (stock solution) flow.
  • a solid phase fluid medium or precipitate such as glass beads
  • a gas phase vapor
  • a liquid phase stock solution
  • the “second heat exchanger” is a three-phase fluidized bed
  • the heat of the pressurized steam is efficiently exchanged with the heat of the latent heat of evaporation of the stock solution and the sensible heat of the steam evaporated from the stock solution.
  • the stock solution can be reliably concentrated.
  • the cleanliness of the heat exchange surface is maintained by allowing it to flow during the concentration operation of the internal stock solution, and stable, even under conditions where the concentrate is concentrated to a high concentration, by scaling to the heat exchange surface Reduction in thermal efficiency can be suppressed.
  • a three-phase fluidized bed 15 connected to the first heat exchanger 5 by a stock solution supply unit 17, a steam supply unit 19, and a discharge unit 21. Can be mentioned. Furthermore, a heat transfer tube 15 is disposed in the heat transfer region inside the three-phase fluidized bed 7.
  • the “three-phase fluidized bed 7” is installed so that the axial direction of the cylinder is the vertical direction, and is formed in a cylindrical shape.
  • the amount of sensible heat of the vapor evaporated from is sufficiently exchanged, so that temperature unevenness can be made difficult to occur. That is, it is difficult to cause quality deterioration due to temperature unevenness, and a high-quality product can be obtained.
  • the “three-phase fluidized bed 7” is made of metal. If it is made of metal, it is possible to make it difficult for temperature unevenness to occur. Therefore, control of temperature rise and temperature fall can be facilitated, and processing can be performed in a short time. Furthermore, thermal efficiency can be improved and running cost can be reduced.
  • Examples of the metal include SUS304, SUS316 (L), SUS310S, titanium, Hastelloy (registered trademark), Inconel (INCONEL: registered trademark), Incoloy (registered trademark), and the like. This is because these metals are excellent in heat resistance and durability against corrosion.
  • the flow rate of pressurized steam fed from the “steam recompressor 3” into the “three-phase fluidized bed 7” is preferably 1 to 20 m / s, more preferably 3 to 15 m / s, and 5 to 10 m. / S is most preferred.
  • the flow rate of the concentrated water passing through the separator and the moisture condensed by the heated steam sent from the “three-phase fluidized bed 7” to the “first heat exchanger 5” is preferably 1 to 20 m / s. -15 m / s is more preferable, and 5 to 10 m / s is most preferable.
  • the temperature of the pressurized steam sent from the “steam recompressor 3” into the “three-phase fluidized bed 7” is preferably 110 to 130 ° C., more preferably 115 to 125 ° C. in the case of a steam compression blower. Preferably, 117 ° C to 123 ° C is most preferable.
  • the pressure steam is preferably 130 to 150 ° C, more preferably 135 to 145 ° C, and most preferably 137 to 143 ° C.
  • the temperature of the pressurized steam sent from the “steam recompressor 3” into the “three-phase fluidized bed 7” is less than 110 ° C. in the case of a steam compression blower, or a steam compressor In this case, if it is less than 130 ° C., a large heat transfer area is required for heat exchange. Further, when the temperature of the pressurized steam fed from the “steam recompressor 3” into the “three-phase fluidized bed 7” is 130 ° C. or more in the case of a steam compression blower, or a steam compressor In this case, if it exceeds 150 ° C., the power in the vapor recompressing device is excessively required, so that the energy efficiency may not be improved.
  • the pressure of the pressurized steam fed from the “steam recompressor 3” into the “three-phase fluidized bed 7” is, for example, 0.14 to 0.27 MPa (absolute pressure in the case of a steam compression blower). ), More preferably 0.17 to 0.23 MPa (absolute pressure), and most preferably 0.18 to 0.21 MPa (absolute pressure).
  • the temperature of moisture condensed from the heated steam sent from the “three-phase fluidized bed 7” to the “first heat exchanger 5” and the temperature of the stock solution concentrated through the separator are preferably 80 to 100 ° C. 85 to 95 ° C is more preferable, and 87 to 93 ° C is most preferable.
  • the moisture condensed from the heated steam sent to the “first heat exchanger 5” from the “three-phase fluidized bed 7” and the stock solution concentrated through the separator have the predetermined temperature, so that The “first heat exchanger 5” can be sufficiently heated. This makes it possible to efficiently exchange the amount of sensible heat of the liquid concentrate and the amount of sensible heat of the liquid after the pressurized steam is condensed, and the amount of sensible heat of the concentrate after the concentrate is concentrated. Can be exchanged efficiently, so there is little energy loss and the stock solution can be concentrated easily.
  • the temperature of the moisture condensed by the heated steam sent from the “three-phase fluidized bed 7” to the “first heat exchanger 5” and the temperature of the stock solution concentrated through the separator are less than 80 ° C. If there is, the amount of water droplets condensed from the steam increases. For this reason, the amount of moisture condensed by the heated steam sent from the “three-phase fluidized bed 7” to the “first heat exchanger 5” and the concentrated concentrate passing through the separator is reduced. There may be a case where the sensible heat exchange is not sufficiently performed in the exchanger 5 ".
  • the temperature of moisture condensed from the heated steam sent from the “three-phase fluidized bed 7” to the “first heat exchanger 5” and the temperature of the stock solution concentrated through the separator are over 100 ° C.
  • the concentration operation is performed, the stock solution may be thermally deteriorated.
  • the second heat exchanger preferably includes a heat transfer region for concentrating the raw material. Furthermore, the heat transfer area of the “heat transfer region” is more preferably formed to be changeable. If the heat transfer area of the heat transfer region can be changed, an optimal heat transfer area can be secured according to the properties of the stock solution.
  • the heat transfer region examples include a heater, a heat transfer tube, and the like. Furthermore, the heat transfer area can be changed by providing the heat transfer area with a structure such as a plurality of heater elements and heat transfer tubes as the heat transfer area of the “heat transfer area” can be changed. .
  • the “heat transfer region” is disposed on the lower side (lower part) in the vertical direction of the three-phase fluidized bed.
  • a steam circulation means that uses the steam generated in the process of evaporating the water in the stock solution as the fluidizing gas of the second heat exchanger.
  • stock solution can be used as fluidization gas, energy efficiency is improved more, and the inside of a 2nd heat exchanger is made to flow by a blower. Scaling on the heat exchange surface can be suppressed, and the heat exchange surface can be kept clean even when the stock solution is concentrated to a high concentration. Thereby, even in a state where the stock solution is concentrated to a high concentration, it is possible to operate stably and realize energy saving.
  • the blower it is preferable to use a model having a discharge pressure of 5 kPa or more.
  • a fluidizing means that uses the steam generated in the process of evaporating the water in the stock solution as the fluidizing gas for the second heat exchanger, the water in the stock solution is evaporated, It is preferable to use a partially branched vapor as the fluidizing gas. That is, by providing a circulation line in the path of the second heat exchanger, it is not necessary to newly provide a complicated device, and the steam generated in the process of evaporating the water in the stock solution can be used as the fluidizing gas.
  • the “second heat exchanger” preferably fluidizes the stock solution.
  • thermal efficiency can be improved by fluidizing the stock solution.
  • fluidizing the stock solution it is possible to prevent scaling of the surface portion that is in contact with the stock solution of the “second heat exchanger”, and further, the stock solution is concentrated to a high concentration by flowing the stock solution. There is a merit that the heat exchange surface can be kept clean even in a wet state.
  • Retransmission means Furthermore, it is preferable to have a retransmission means for concentrating the stock solution and retransmitting the obtained concentrated stock solution to one of the second heat exchanger and the first heat exchanger.
  • FIG. 1 shows an example in which the concentrated stock solution is retransmitted to the first heat exchanger.
  • the concentrated stock solution obtained by concentrating the stock solution and resending the obtained concentrated stock solution to one of the second heat exchanger and the first heat exchanger is preferably 1 to 20 m / s. 15 m / s is more preferable, and 5 to 10 m / s is most preferable.
  • the concentrating device includes stock solution supplying means for supplying the stock solution to the concentrating device, and steam supplying means for supplying the steam to the concentrating device.
  • stock solution supply means is means for feeding the stock solution to the first heat exchanger and the second heat exchanger.
  • stock solution supply means is composed of, for example, a stock solution inlet, a stock solution supply pump, a stock solution supply pipe, and the like. Specifically, the stock solution stored in the stock solution tank or the like passes through the pipe laid from the stock solution tank, passes through the stock solution supply pump, and is supplied from the stock solution supply pipe to the first heat exchanger and the second heat exchanger.
  • the “steam supply means” is means for supplying steam into the second heat exchanger.
  • the steam supply means includes a blower, a steam supply pump, a steam compressor, and the like.
  • First discharge means second discharge means: (First discharge means) Further, the “concentrator” includes first discharge means for discharging the “concentrate” obtained by concentrating the stock solution to the outside. By providing the “first discharging means”, the concentrated solution obtained by efficiently concentrating the stock solution or the precipitates inside the stock solution can be discharged to the outside.
  • the “first discharge means” is composed of, for example, a discharge pipe, a discharge pump, and a tank. As a specific configuration of the “first discharge means”, the discharge pipe installed in the second heat exchanger passes through a pipe laid and is collected into a tank via a discharge pump.
  • the “first discharging means” may discharge the “concentrated liquid” or “precipitate inside the stock solution” outside by a pressure discharging method or an overflow discharging method.
  • the “concentrator” includes a second discharge means for discharging the liquid after the pressurized vapor is condensed.
  • a second discharge means for discharging the liquid after the pressurized steam is condensed.
  • the “second discharge means” includes, for example, a discharge pipe, a discharge pump, and a tank. As a specific configuration of the “exhaust means”, it passes through a pipe laid from an exhaust pipe installed in the second heat exchanger, and is collected into a tank through an exhaust pump.
  • the “second discharging means” may discharge the above “liquid after the pressurized steam is condensed” to the outside by a pressure discharging method or an overflow discharging method.
  • the concentration of the stock solution concentrated by the concentration apparatus of the present invention is preferably 3 to 10%.
  • stock solution concentrated with a concentrating device means the 100 fraction of the mass (kilogram) of the raw material melt
  • concentration of the raw material is 3 to 10%, handling becomes easy as a property used for the concentration operation.
  • concentration of the raw material is less than 3%, the amount of water to be evaporated increases and the energy consumption increases.
  • concentration of the raw material is not limited to the meaning of the concentration of the stock solution before the concentration treatment, but also includes the concentration of the concentrate produced after the concentration treatment.
  • Raw material of the concentrate to be concentrated
  • stock solutions produced by an extraction operation such as pharmaceuticals including herbal medicine, sugars, dairy products, and plant extracts.
  • the raw material is supplied into the three-phase fluidized bed 7.
  • the stock solution supply device include a pressure nozzle, a pressure two-fluid nozzle and the like in addition to a two-fluid nozzle installed in the upper part of the three-phase fluidized bed 7.
  • the other stock solution supply device include a dropping type supply pipe, a dropping nozzle, a liquid feeding pipe forcibly feeding the fluid into the fluidized bed, and the like.
  • the concentration method in the present invention generally has a pressurized steam generation step, a first heat exchange step, and a second heat exchange step, and further includes a stock solution supply step, a steam supply step, a first discharge step, a water droplet separation step, a first A concentration method for concentrating the stock solution.
  • the “pressurized steam generation step” is a step of generating pressurized steam obtained by pressurizing the steam.
  • the “pressurized steam generation step” is a step of generating pressurized steam obtained by pressurizing the steam.
  • the “first heat exchange step” includes the amount of liquid sensible heat of the stock solution to be concentrated, the amount of heat of liquid sensible heat after the pressurized steam is condensed, and the amount of sensible heat of the concentrated solution in which the stock solution is concentrated. This is a process of exchanging the amount of heat.
  • the “second heat exchange step” is a step in which the amount of heat of the pressurized steam, the amount of latent heat of evaporation of the stock solution, and the sensible heat of vapor evaporated from the stock solution can be exchanged, and the stock solution can be concentrated.
  • the “stock solution supply step” is a step of supplying the stock solution to the first heat exchange step and further supplying the stock solution from the first heat exchange step to the second heat exchange step.
  • the “steam supply step” is a step of supplying the vapor evaporated from the stock solution to the second heat exchange step.
  • the “first discharge step” is a step of discharging the concentrated liquid obtained by concentrating the stock solution to the outside.
  • the “water droplet separation step” is a step of separating water droplets that have flowed out of the second heat exchange step and mixed in the vapor evaporated from the stock solution.
  • the “second discharge step” is a step of discharging the liquid after the pressurized vapor is condensed.
  • the concentration operation can be performed by the self-heat regeneration technology by the pressurized steam generation process for generating the pressurized steam by pressurizing the steam. Furthermore, in the concentration method of the present invention, a highly efficient concentration operation can be realized by exchanging all of liquid sensible heat, latent heat of vaporization, and vapor sensible heat in the concentration / evaporation process. In addition, since only the temperature difference required for heat exchange becomes the energy required as power, the concentration process using the concentration method of the present invention can perform the concentration process without requiring a new heating operation. To do.
  • pressurized steam obtained by pressurizing steam is preferably steam generated in the process of evaporating the stock solution.
  • a vapor different from the vapor generated in the process of evaporating the stock solution may be used, but at least the steam generated in the process of evaporating the stock solution is preferably used in the treatment process.
  • the higher the proportion of steam generated in the process of evaporating the stock solution the more energy efficiency can be improved. Therefore, the steam is more likely to be generated in the process of evaporating the stock solution. preferable.
  • “exchange the amount of heat of the pressurized steam and the amount of heat of the stock solution to be concentrated” refers to “concentrated concentrate” and “concentrated solution” from “supply of stock solution”. Means the exchange of the calorific value of each stage of the “pressure steam calorie” and the “stock solution for concentrating” in the process leading to the discharge of the “condensed liquid of pressurized steam” To do.
  • the concentration method of the present invention has a circulation step in which sensible heat or latent heat, or both sensible heat and latent heat are circulated in any of the pressurized steam generation step, the heat exchange step, and the vapor recompression step.
  • Such a configuration eliminates the need for complicated processing steps, allows the vapor generated in the process of evaporating the water in the stock solution to be used as a fluidizing gas, improves energy efficiency, and promotes the concentration operation.
  • concentration apparatus and concentration method The specific aspect about the concentration apparatus and concentration method of this invention demonstrated until now is demonstrated. However, it is not limited to the concentration apparatus and the concentration method described below.
  • the concentrator 1 includes a compressor 3, a first heat exchanger 5, a second heat exchanger 7, a stock solution supply unit 17, a blower 13, and a three-phase fluidized bed 7.
  • the stock solution to be concentrated is introduced into the supply port 17 a of the stock solution supply means 17 and stored in the “stock solution tank 17 a” constituting the stock solution supply means 17.
  • a predetermined amount is sent to the “first heat exchanger 5” by the pump P.
  • the heated “stock solution” is sent to the “second heat exchanger 7” via the “stock solution supply pipe 17 c” constituting the stock solution supply means 17.
  • sensible heat exchange is performed between the amount of liquid sensible heat of the stock solution to be concentrated and the amount of sensible heat of the liquid after the pressurized steam is condensed, and the stock solution is concentrated. The sensible heat of the concentrated liquid after the sensible heat is exchanged with the sensible heat, and the stock solution is heated.
  • the stock solution heated in the “first heat exchanger 5” passes through the “stock solution supply pipe 17 c” constituting the stock solution supply unit 17 to the “second heat exchanger”. 7 ”.
  • the “second heat exchanger 7” is a three-phase fluidized bed
  • the temperature is raised in the “first heat exchanger 5” fed into the “three-phase fluidized bed 7”.
  • the moisture of the stock solution evaporates or is concentrated by the amount of heat of “steam heated by the compressor 3” sent into the three-phase fluidized bed 7. That is, “the moisture (vapor)” when the moisture in the stock solution evaporates with the heat quantity of the steam heated by the compressor 3 is further heated by the adiabatic compression operation of the compressor 3.
  • a part of the raw liquid water evaporated to become a vapor is not passed through the compressor 3, but is passed through the second circulation line 11 by the blower 13. It is sent again to the phase fluidized bed 7.
  • the heat exchange between the steam and the stock solution is sufficiently performed in the three-phase fluidized bed 7. become. That is, the steam compressed (heated) by the compressor 3 is sent to the second heat exchanger 7 via the first circulation line 9 and further provided inside the second heat exchanger 7. The heat exchange is performed with the stock solution in the second heat exchanger 7 through the heat transfer tube.
  • the water that has undergone heat exchange and has condensed the steam is further sent to the first heat exchanger 5, and in the first heat exchanger 5, the water is exchanged with the stock solution sent from the first supply means 17 to the exchanger 5.
  • the Thereafter, the “water” heat-exchanged by the first heat exchanger 5 is discharged from the “concentrator 1” to the collection tank by the second discharge means 23.
  • the concentrated liquid obtained by concentrating the stock solution is discharged from the three-phase fluidized bed 7 through the first discharge pipe of the first discharge means 21 to the outside.
  • the concentrated liquid recovery tank 21a and the auxiliary tank 21b may be installed in the first discharge means 21 to store the concentrated liquid obtained by concentrating the stock solution.
  • symbol X shown in FIG. 1 shows the flow of water vapor
  • symbol Y indicates the flow of water in the “concentrator”.
  • symbol “M” indicates a motor, and symbol P indicates “pump”.
  • Example 1 As shown in FIG. 1, a steam recompressor, a first heat exchanger, a second heat exchanger, a raw solution supply means, a steam supply means, a first discharge means, a second discharge means, a water droplet separation means are arranged, A concentrator was prepared.
  • the liquid stored in the stock solution tank was supplied to the first heat exchanger and the second exchanger by a liquid feed pump. At this time, the temperature of the liquid to be fed was set to 25 ° C. Furthermore, a 10% by mass dextrin aqueous solution was used as a target liquid for concentration.
  • concentration of dextrin aqueous solution means the 100 fraction of the mass (kilogram) of dextrin melt
  • the state of the raw material was 91 ° C. at the outlet of the first heat exchanger.
  • the state of the steam at the outlet of the second heat exchanger for exchanging latent heat and steam sensible heat was 101 ° C. and 0.1 MPa.
  • steam was pressurized with the vapor
  • the pressurized steam was supplied again to the second heat exchanger, and heat exchange was performed with the newly supplied raw material. Further, a part of the steam was separated and used as a flowing gas for the second heat exchanger.
  • steam sensible heat and latent heat are heat-exchanged in the second heat exchanger, and the state at the outlet of the second heat exchanger is 110 ° C.
  • the sensible heat was heat-exchanged in the first heat exchanger and recovered as distilled water in the recovery tank.
  • the heat transfer area of the heat transfer area in the second heat exchanger is insufficient and good heat exchange was not performed, but after that, a suitable heat transfer area can be selected and good operation can be performed. It has become possible.
  • the concentration of the obtained stock solution was confirmed during operation, it was lower than the design value. Therefore, a part of the stock solution was retransmitted to the first heat exchanger by the re-transmission means.
  • a stock solution having a concentration as designed was obtained at a flow rate of 12 kg / h. Under this condition, the energy required for vapor recompression was 1.8 kW.
  • Example 1 A vapor recompressor, a first heat exchanger, a second heat exchanger, and a vapor supply means were excluded from the concentrator as shown in FIG.
  • a liquid feed pump With a liquid feed pump, the liquid was fed to the evaporation container under conditions of a liquid feed temperature of 25 ° C. and a flow rate of 30 kg / h.
  • a heater As a liquid heating method, a heater was used, and the same operation as in Example 1 was performed except that steam recompression heat exchange and heat exchange were performed. Operation was performed under these conditions, and a concentrated liquid was obtained at a flow rate of 12 kg / h. When the energy required for operation was calculated, the amount of heat required for evaporation of the raw material liquid was 13 kW.
  • Example 1 In Example 1, the amount of heat required for evaporation of the raw material was dramatically lower than that in Comparative Example 1, and the energy saving effect was sufficiently exhibited. Therefore, this proves the effect of the present invention. In addition, by changing the heat transfer area, it was possible to select a condition for keeping the energy consumption to a minimum, while in Comparative Example 1, the energy saving property was poor and the thermal efficiency was low.
  • Example 2 As shown in FIG. 1, a steam recompressor, a first heat exchanger, a second heat exchanger, a raw solution supply means, a steam supply means, a first discharge means, a second discharge means, a water droplet separation means are arranged, A concentrator was prepared. A 10% by mass dextrin aqueous solution stored in the stock solution tank was supplied to the second exchanger by a liquid feed pump. At this time, the temperature of the liquid to be fed was set to 25 ° C. In this state, the heat exchanger was operated, and a 10% by mass dextrin aqueous solution was caused to flow in the second exchanger.
  • FIG. 2 A concentrator excluding the steam supply means from the concentrator as shown in FIG. 1 was prepared.
  • a 10% by mass dextrin aqueous solution stored in the stock solution tank was supplied to the second exchanger by a liquid feed pump. At this time, the temperature of the liquid to be fed was set to 25 ° C. In this state, the heat exchanger was operated, and a 10% by mass dextrin aqueous solution was concentrated in the second exchanger.
  • water in the 10% by mass dextrin aqueous solution evaporated and the concentration operation proceeded, dextrin deposited on the surface of the heat exchanger in contact with the 10% by mass dextrin aqueous solution inside the second heat exchanger.
  • Example 2 In Example 2, since the 10 mass% dextrin aqueous solution inside the second heat exchanger 7 flows, scale precipitation on the surface of the heat exchanger was not observed, and a decrease in heat transfer efficiency was suppressed. . Therefore, this proves the effect of the present invention. On the other hand, in Comparative Example 2, due to the scaling of the heat exchanger surface, the energy saving performance was poor and stable operation could not be performed.
  • the concentration apparatus and concentration method of the present invention can be used for concentration of a stock solution.
  • a concentration apparatus and a concentration method capable of realizing a highly efficient heat exchange operation are provided.
  • a heating operation is unnecessary.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention concerne un dispositif de concentration et un procédé de concentration aptes à réduire une consommation d'énergie à la moitié ou moins par rapport au procédé flash multi-étages classique. Plus précisément, par utilisation d'un lit fluidisé à trois phases, le dispositif de concentration et le procédé de concentration rendent possible un fonctionnement à rendement thermique élevé, rendent possible d'éviter une mise à l'échelle sur une surface de transmission de chaleur, et rendent possible un fonctionnement lorsque la concentration de solution de réserve est élevée. Ce dispositif de concentration (1) pour concentrer une solution de réserve comprend : un re-compresseur de vapeur (3) apte à produire de la vapeur sous pression par pressurisation de vapeur ; un premier échangeur thermique (5) apte à échanger de la chaleur entre la quantité de chaleur sensible du liquide dans la solution de réserve à concentrer, la quantité de chaleur sensible du liquide après que la vapeur sous pression est condensée, et la quantité de chaleur sensible dans le liquide concentré obtenu par concentration de la solution de réserve ; un second échangeur thermique (7) apte à concentrer la solution de réserve et apte à échanger de la chaleur entre la quantité de chaleur dans la vapeur sous pression, la quantité de chaleur latente due à la vaporisation de la solution de réserve, et la quantité de chaleur sensible dans la vapeur obtenue par vaporisation de la solution de réserve ; un moyen de fourniture de solution de réserve (17) ; un moyen d'alimentation en vapeur (19) ; un premier moyen de décharge (21) ; un moyen de séparation de gouttelettes d'eau (25) ; et un second moyen de décharge (23).
PCT/JP2014/065007 2013-06-05 2014-06-05 Dispositif de concentration et procédé de concentration WO2014196611A1 (fr)

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CN109589629A (zh) * 2019-01-30 2019-04-09 杭州胡庆余堂天然食品有限公司 一种黏稠膏滋的蒸汽再压缩节能浓缩装置及方法

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JP2002515336A (ja) * 1998-05-14 2002-05-28 アクア・ピュア・ベンチャーズ・インコーポレイテッド 機械的蒸気再圧縮プロセス
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JP2006334532A (ja) * 2005-06-03 2006-12-14 Sasakura Engineering Co Ltd 濃縮装置
JP4592700B2 (ja) * 2004-09-02 2010-12-01 有限会社アクアシステムズ 機械的蒸気圧縮法による単段フラッシュ蒸発法海水淡水化装置に用いる蒸発室

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JPS6380469U (fr) * 1986-11-12 1988-05-27
JP2002515336A (ja) * 1998-05-14 2002-05-28 アクア・ピュア・ベンチャーズ・インコーポレイテッド 機械的蒸気再圧縮プロセス
JP2002105039A (ja) * 2000-09-29 2002-04-10 Sumitomo Chem Co Ltd シクロヘキサノンオキシムの蒸発方法とこれに使用する蒸発器、ならびにε−カプロラクタムの製造方法とその製造装置
JP2006507941A (ja) * 2002-11-13 2006-03-09 デカ プロダックツ リミテッド パートナーシップ 蒸気圧縮を用いた蒸留法
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JP2006334532A (ja) * 2005-06-03 2006-12-14 Sasakura Engineering Co Ltd 濃縮装置

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109589629A (zh) * 2019-01-30 2019-04-09 杭州胡庆余堂天然食品有限公司 一种黏稠膏滋的蒸汽再压缩节能浓缩装置及方法

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